Use of supported lead oxide catalyst in the preparation of tertiary butyl alcohol from tertiary butyl hydroperoxide

Description

[0001] This invention relates to the catalytic decomposition of tertiary butyl hydroperoxide (TBHP). More particularly, this invention relates to a method for the preparation of tertiary butyl alcohol (TBA) by the catalytic decomposition of tertiary butyl hydroperoxide. Still more particularly, this invention relates to a method wherein an alumina supported lead oxide catalyst is used to catalyze the substantially selective decomposition of tertiary butyl hydroperoxide to tertiary butyl alcohol.

[0002] It is known to react isobutane with oxygen, either thermally or catalytically, to form a peroxidation reaction product wherein the principal peroxide that is formed is tertiary butyl hydroperoxide. It is also known to thermally or catalytically decompose the tertiary butyl hydroperoxide to form tertiary butyl alcohol.

[0003] Sanderson et al. disclose the use of a variety of catalysts for the decomposition of tertiary butyl hydroperoxide in a series of U. S. patents, including a catalyst composed of unsupported nickel, copper, chromia and iron (U. S. Patent No. 4,704,482), a catalyst composed of iron, copper, chromia and cobalt (U. S. Patent No. 4,705,903), a catalyst composed of a base treated hydrogenation catalyst from groups VIA or VIII of the Periodic Table (U. S. Patent No. 4,742,179), a catalyst consisting essentially of nickel, copper, chromium and barium (U. S. Patent No. 4,873,380), a catalyst composed of a metal phthalocyanine promoted with a rhenium compound (U. S. Patent No. 4,910,349), a catalyst composed of a base promoted metal phthalocyanine compound (U. S. Patent No. 4,912,269), a catalyst composed of a soluble ruthenium compound promoted with a bidentate ligand (U. S. Patent No. 4,912,033), a catalyst composed of a metal porphine such as iron (III) or manganese (III) promoted with an alkyl thiol or an amine, a catalyst composed of an imidazole promoted metal phthalocyanine compound (U. S. Patent No. 4,912,266), (U. S. Patent No. 4,922,034), a catalyst composed of a metal phthalocyanine promoted with a thiol and a free radical inhibitor (U. S. Patent No. 4,922,035), a catalyst composed of a borate promoted metal phthalocyanine (U. S. Patent No. 4,922,036), or a catalyst composed of a soluble ruthenium compound and an iron compound such as an acetate, a borate, a bromide, a chloride, a 1,3-propanedionate, a 2-ethyl-hexanoate, an iodide, a nitrate, a 2,4-pentanedionate, a perchlorate or a sulfate (U. S. Patent No. 5,025,113).

[0004] As stated, when isobutane is reacted with molecular oxygen, the principal products of the reaction are tertiary butyl alcohol and tertiary butyl hydroperoxide. However, minor amounts of other contaminants are also formed. A minor amount of water will be formed, which will normally amount to 0.5 to 1 wt.% of the reactor effluent. The amount of byproduct water that is produced is a function of the severity of the reaction conditions employed and will tend to increase as the severity of the reaction conditions is increased.

[0005] As indicated, tertiary butyl hydroperoxide is useful as a raw material for the manufacture of tertiary butyl alcohol. The tertiary butyl alcohol can be formed by catalytic decomposition of the tertiary butyl hydroperoxide. US-A-3,472,876 discloses a process wherein an oxygen-containing gas was charged to a reactor containing isobutane and an oxidation catalyst to provide a reaction mixture comprising tertiary butyl alcohol, tertiary butyl hydroperoxide, acetone, and tertiary butyl ether. The reported results in the patent indicate that there was a comparatively low rate of conversion and a comparatively poor selectivity of the reaction to tertiary butyl alcohol.

[0006] There is a need for a catalytic decomposition of tertiary butyl hydroperoxide to tertiary alcohol at a higher conversion rate and an improved selectivity over the prior art.

[0007] In accordance with the present invention, a solvent solution of a tertiary butyl hydroperoxide charge stock is brought into contact with a catalytically effective amount of a hydroperoxide decomposition catalyst in a hydroperoxide decomposition reaction zone in liquid phase, preferably with agitation, to convert the tertiary butyl hydroperoxide to decomposition products, principally tertiary butyl alcohol, the hydroperoxide decomposition catalyst consisting essentially of alumina having from 0.5 to 25 wt.% of lead oxide deposited thereon. Tertiary butyl alcohol is recovered from the products of the hydroperoxide decomposition reaction.

[0008] The tertiary butyl alcohol will not be the only decomposition product that is formed. Minor amounts of other oxygen-containing materials such as those listed above will also be formed.

[0009] The starting materials for the process of the present invention are a tertiary butyl hydroperoxide feedstock and an alumina supported lead oxide catalyst.

The Tertiary Butyl Hydroperoxide Feedstock

[0010] The tertiary butyl hydroperoxide charge stock may comprise an isobutane oxidation product wherein the tertiary butyl hyroperoxide is dissolved in a mixture of isobutane and tertiary butyl alcohol or may comprise an isobutane oxidation product enriched by the addition of tertiary butyl alcohol, such that the solution of tertiary butyl alcohol in the mixture of isobutane with tertiary butyl alcohol contains from 5 to 30 wt.% of tertiary butyl hydroperoxide.

[0011] Alternatively, the isobutane reaction product may be charged to a distillation zone where unreacted isobutane is removed as a distillate fraction for recycle to thereby provide a solution of tertiary butyl hydroperoxide in tertiary butyl alcohol containing 5 to 30 wt.% of tertiary butyl hydroperoxide.

The Catalyst System

[0012] The hydroperoxide decomposition catalyst to be used in accordance with the present invention consists essentially of alumina having from about 0.5 to about 25 wt.% of lead oxide deposited thereon.

Catalytic Decomposition of Tertiary Butyl Hydroperoxide

[0013] The process of the present invention may be conducted batchwise in kettles or by continuously passing the reactants through a tubular reactor.

[0014] The catalytic decomposition of the tertiary butyl hydroperoxide is preferably conducted at a temperature within the range of 20° to 250°C, preferably 60° to 120°C, and more preferably, at a temperature within the range of 80° to 100°C. The reaction is preferably conducted at a pressure sufficient to keep the reactants and the reaction products in liquid phase. A pressure of 0.1 to 69 MPa (0 to 10,000 psig), preferably 0.1 to 7.0 MPa (0 to 1000 psig) may be used, if desired.

[0015] Flow rates of the charge solution to the reaction zone should be adjusted in order to provide an appropriate contact time within the reactor. In a batch process, the holding time may suitably be from 0.5 to 10 hours, and more preferably 1 to 3 hours.

[0016] In accordance with a preferred embodiment of the present invention, isobutane is reacted with oxygen in an oxidation zone under oxidation reaction conditions including a temperature of 135 to 155°C., a pressure of 2.1 to 5.6 MPa (300 to 800 psig), and a holding time of 2 to 6 hours to provide an initial oxidation reaction product comprising unreacted isobutane, tertiary butyl hydroperoxide, tertiary butyl alcohol, and oxygen-containing by-products. The initial oxidation reaction product is then used as the tertiary butyl hydroperoxide charge stock of the present invention. If the concentration of tertiary butyl hydroperoxide in the tertiary butyl hydroperoxide charge stock is more than 30 wt.% of the initial oxidation reaction product, the initial oxidation reaction product can be diluted with an amount of tertiary butyl alcohol sufficient to lower the concentration of the tertiary butyl hydroperoxide to a desired percentage, to provide, for example, a tertiary butyl hydroperoxide charge stock containing from 15 to 25 wt.% of tertiary butyl hydroperoxide.

[0017] Alternatively, the initial oxidation reaction product may be fractionated in any appropriate manner (e.g., by distillation in a distillation zone) to remove the isobutane therefrom for recycle and to provide a solution of tertiary butyl hydroperoxide and tertiary butyl alcohol which will normally contain from 5 to 30 wt.% of tertiary butyl hydroperoxide.

[0018] The solution of tertiary butyl hydroperoxide in tertiary butyl alcohol is then charged to a catalytic hydroperoxide decomposition zone where it is brought into contact with an alumina supported lead oxide catalyst to substantially selectively convert the tertiary butyl hydroperoxide to tertiary butyl alcohol with high yields and selectivities.

[0019] When the process of the present invention is practiced in a continuous manner by continuously charging the tertiary butyl hydroperoxide charge stock to a reactor containing a fixed bed of pelleted hydroperoxide decomposition catalyst, the space velocity is suitably in the range of 0.5 to 3 volumes of tertiary butyl hydroperoxide charge stock per volume of catalyst per hour. Preferably, the space velocity is within the range of 1 to 2 volumes of tertiary butyl hydroperoxide charge stock per volume of catalyst per hour.

[0020] The reaction product from the tertiary butyl hydroperoxide decomposition step may then be fractionated in any suitable manner, such as by distillation to recover the tertiary butyl alcohol.

EXAMPLES

[0021] The invention will be further illustrated by the following non-limiting examples.

Procedure

[0022] The reactor that was used for the experiments was a stainless steel tube (12.3 x 360mm) which was electrically heated. Liquid feed was pumped into the bottom of the reactor using a Ruska® dual drive pump. Pressure was regulated using a Skinner Uni-Flow® valve and a Foxboro® controller. Samples were collected at the top of the reactor, cooled to ambient temperature, filtered and analyzed by Gas Chromatography. The analysis of the feed and of the products obtained is reported in the following tables.

Example 1

[0023] In this example, the catalyst consisted essentially of lead oxide supported on alumina.

TABLE 1

CATALYTIC CONVERSION OF TERT-BUTYLHYDROPEROXIDE TO TERT-BUTYLALCOHOL
RUN	A	1	2	3	4
Catalyst		PbO on Al₂O₃	PbO on Al₂O₃	PbO on Al₂O₃	PbO on Al₂O₃
Catalyst (cc)		100	100	100	100
Pressure (MPa)		3.5	3.5	3.5	3.5
Feed Rate (cc/Hr.)		50	50	50	50
Temperature (°C)		80	100	120	140
Time on Stream (Hr)		4	4	4	4
Space Vel. (cc/cc)		0.5	0.5	0.5	0.5
TBHP Conversion (mol.%)		72.5	82.1	95.0	98.3
Selectivity IC4= (mol.%)		-0.0	0.0	-0.0	0.0
Sel. Acetone (mol.%)		8.5	14.0	18.7	27.9
Sel. Methanol (mol.%)		1.4	2.6	5.0	8.0
Sel. TBA (mol.%)		83.9	80.3	78.1	70.9
Sel. DTBP (mol.%)		7.7	5.7	3.2	1.3

Remarks	H₂O Free Basis	H₂O Free Basis	H₂O Free Basis	H₂O Free Basis	H₂O Free Basis
Composition, wt%
IC4=	0.001	0.000	0.001	0.000	0.002
MEOH/MF	0.016	0.083	0.162	0.337	0.552
Acetone	0.008	0.765	1.429	2.206	3.385
TBA	79.968	92.463	93.740	95.496	95.005
DTBP	0.055	0.917	0.785	0.521	0.251
TBHP	19.146	5.270	3.419	0.948	0.333

TABLE 2

CATALYTIC CONVERSION OF TERT-BUTYLHYDROPEROXIDE TO TERT-BUTYLALCOHOL
RUN	A	5	6	7	8
Catalyst		PbO on Al₂O₃	PbO on Al₂O₃	PbO on Al₂O₃	PbO on Al₂O₃
Catalyst (cc)		100	100	100	100
Pressure (MPa)		3.5	3.5	3.5	3.5
Feed Rate (cc/Hr.)		100	100	100	100
Temperature (°C)		80	100	120	140
Time on Stream (Hr)		4	4	4	4
Space Vel. (cc/cc)		1.0	1.0	1.0	1.0
TBHP Conversion (mol.%)		15.3	40.8	83.4	97.3
Selectivity IC4= (mol.%)		-0.1	-0.0	-0.0	0.0
Sel. Acetone (mol.%)		11.1	12.0	18.1	35.5
Sel. Methanol (mol.%)		1.9	2.6	5.8	10.5
Sel. TBA (mol.%)		80.9	82.0	79.2	64.0
Sel. DTBP (mol.%)		8.0	6.0	2.7	0.5

Remarks	H₂O Free Basis	H₂O Free Basis	H₂O Free Basis	H₂O Free Basis	H₂O Free Basis
Composition, wt%
IC4=	0.001	0.000	0.000	0.000	0.004
MEOH/MF	0.016	0.036	0.088	0.343	0.713
Acetone	0.008	0.216	0.612	1.872	4.275
TBA	79.968	82.443	86.692	93.593	93.536
DTBP	0.055	0.245	0.438	0.401	0.127
TBHP	19.146	16.226	11.335	3.176	0.518

TABLE 3

CATALYTIC CONVERSION OF TERT-BUTYLHYDROPEROXIDE TO TERT-BUTYLALCOHOL
RUN	A	9	10	11
Catalyst		PbO on Al₂O₃	PbO on Al₂O₃	PbO on Al₂O₃
Catalyst (cc)		100	100	100
Pressure (MPa)		3.5	3.5	3.5
Feed Rate (cc/Hr.)		200	200	200
Temperature (°C)		100	120	140
Time on Stream (Hr)		4	4	4
Space Vel. (cc/cc)		2.0	2.0	2.0
TBHP Conversion (mol.%)		30.5	77.3	92.3
Selectivity IC4= (mol.%)		-0.0	0.0	-0.0
Sel. Acetone (mol.%)		12.7	20.1	29.8
Sel. Methanol (mol.%)		2.5	6.0	11.0
Sel. TBA (mol.%)		82.5	77.2	69.3
Sel. DTBP (mol.%)		4.8	2.7	0.9

Remarks	H₂O Free Basis	H₂O Free Basis	H₂O Free Basis	H₂O Free Basis
Composition, wt%
IC4=	0.001	0.000	0.001	0.000
MEOH/MF	0.016	0.068	0.333	0.708
Acetone	0.008	0.488	1.926	3.398
TBA	79.968	84.992	92.240	93.509
DTBP	0.055	0.281	0.379	0.191
TBHP	19.146	13.297	4.354	1.474

[0024] A 19.1% solution of TBHP in TBA was converted in good yield to TBA over a heterogenous lead oxide on alumina catalyst. For example, at 80°C using a 100 cc reactor and a space velocity of 0.5, a 72.5% conversion of TBHP was obtained with the following selectivities: TBA 83.9%; DTBP 7.7%; acetone 8.5%; methanol 1.4%.

Claims

1. A method for the decomposition of tertiary butyl hydroperoxide to tertiary butyl alcohol, wherein a solvent solution of tertiary butyl hydroperoxide charge stock is brought into contact with a hydroperoxide decomposition catalyst, characterized in that said hydroperoxide decomposition catalyst comprises lead oxide supported on alumina.

2. A method as claimed in Claim 1, wherein the solvent comprises tertiary butyl alcohol, or a mixture thereof with isobutane.

3. A method as claimed in Claim 1 or Claim 2, wherein a solution of a tertiary butyl hydroperoxide charge stock that contains from 5 to 30 wt.% of tertiary butyl hydroperoxide is brought into contact with a catalytically effective amount of a hydroperoxide decomposition catalyst in a hydroperoxide decomposition reaction zone in liquid phase under hydroperoxide conversion conditions including a temperature within the range of 20° to 250°C. and a pressure of 0.1 to 7 MPa (0 to 1,000 psig) to convert said tertiary butyl hydroperoxide to decomposition products, principally tertiary butyl alcohol, characterized in that said hydroperoxide decomposition catalyst consists essentially of alumina having deposited thereon from 0.5 to 25 wt.% of lead oxide.

4. A method as claimed in anyone of Claims 1 to 3, wherein the temperature is in the range of 40° to 150°C. and the pressure is 0.1 MPa.